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Method for producing propylene by catalytic cracking of hydrocarbons

A catalytic cracking and catalytic cracking technology, which is applied in the production of bulk chemicals, hydrocarbon cracking to produce hydrocarbons, and hydrocarbon oil treatment products, etc., can solve problems such as increasing the processing amount of light hydrocarbons, increasing coke yield, and reducing propylene yield

Active Publication Date: 2021-04-27
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

After the MTBE unit is shut down, there will be a large amount of C4 resources that can be used as raw materials for the DCC-plus unit. However, simply increasing the processing capacity of light hydrocarbons will lead to a decrease in the yield of propylene and an increase in the yield of coke

Method used

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  • Method for producing propylene by catalytic cracking of hydrocarbons
  • Method for producing propylene by catalytic cracking of hydrocarbons
  • Method for producing propylene by catalytic cracking of hydrocarbons

Examples

Experimental program
Comparison scheme
Effect test

Embodiment approach

[0033] According to a preferred embodiment of the present invention, the mass ratio of the first regenerated catalyst to the second regenerated catalyst is 2-4:1. Adopting this preferred embodiment is more conducive to producing more propylene.

[0034] According to the present invention, preferably, the operating conditions of the first riser reactor include: the solvent-oil ratio is 8-20, the oil-gas residence time is 0.5-5s, and the outlet temperature is 550-580°C; preferably, the solvent-oil ratio 10-20, the oil and gas residence time is 0.8-2s, and the outlet temperature is 550-570°C.

[0035] According to the present invention, preferably, the operating conditions of the second riser reactor include: the outlet temperature is 610-650°C, the oil and gas residence time is 0.1-4s; more preferably, the outlet temperature is 620-630°C, and the oil and gas residence time The time is 0.5-3s.

[0036] In the present invention, the operating conditions of the fluidized bed reac...

Embodiment 1

[0062] Experiments were carried out using a modified medium-sized device for continuous reaction-regeneration operation, and the process flow is as follows figure 1 Shown, the inner diameter of the first riser reactor 1 of this medium-sized device is 16 millimeters, and the length is 3800 millimeters, and the inner diameter of the second riser reactor 2 is 12 millimeters, and the length is 3200 millimeters, and the inner diameter of the fluidized bed reactor 3 is 64 mm and a height of 600 mm. The high-temperature regenerated catalyst at 700°C is respectively introduced into the bottom of the first riser reactor 1 and the second riser reactor 2 through the first regenerated catalyst delivery pipe 11 and the second regenerated catalyst delivery pipe 21 from the regenerator 6, and is The steam flows upwards. After the heavy raw oil is mixed with atomized water vapor, it enters the first riser reactor 1 through the first feed nozzle 12 to contact with the hot regenerant for catal...

Embodiment 2

[0073] Experiments were carried out using a modified medium-sized device for continuous reaction-regeneration operation, and the process flow is as follows figure 2 Shown, the inner diameter of the first riser reactor 1 of this medium-sized device is 16 millimeters, and the length is 3800 millimeters, and the inner diameter of the second riser reactor 2 is 12 millimeters, and the length is 3200 millimeters, and the inner diameter of the fluidized bed reactor 3 is 64 mm and a height of 600 mm. The bottom of the first riser reactor 1 is provided with a catalyst mixer 7, and the high-temperature regenerated catalyst at 690° C. is introduced into the catalyst mixer through the first regenerated catalyst delivery pipe 11, and part of the ungenerated catalyst is introduced into the catalyst mixer through the ungenerated catalyst circulation pipe 52. Upward flow with pre-lift steam. After the heavy raw oil is mixed with atomized water vapor, it enters the first riser reactor 1 thro...

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Abstract

The invention relates to the field of petroleum refining and petrochemical processing, and discloses a method for producing propylene by catalytic cracking of hydrocarbons, which comprises the following steps: (1) carrying out a first catalytic cracking reaction on heavy raw oil and a first regenerated catalyst to obtain a first oil mixture; (2) carrying out a second catalytic cracking reaction on the light raw oil and a second regenerated catalyst to obtain a second oil agent mixture; and (3) carrying out a third catalytic cracking reaction on the first oil agent mixture and the second oil agent mixture to obtain a third oil agent mixture, and carrying out separation, prerequisite and regeneration for cyclic utilization; wherein the mass ratio of the heavy raw oil to the light raw oil is 0.5-5: 1; the method further comprises the following steps: introducing a first cooling medium into the outlet of the first riser reactor; and / or introducing a second cooling medium into the stripper, and circulating part of the stripped spent catalyst back to the first riser reactor. The method provided by the invention can improve the propylene selectivity and reduce the yields of dry gas and coke.

Description

technical field [0001] The invention relates to the fields of petroleum refining and petrochemical processing, in particular to a method for producing propylene by catalytic cracking of hydrocarbons. Background technique [0002] In 2015, the crude oil processing capacity of domestic catalytic cracking units was about 750 million tons per year, the operating rate of catalytic cracking units was about 70%, and the demand for diesel consumption was at an inflection point. With the further expansion of refining capacity and the popularization of new energy vehicles, the demand for vehicle fuel continues to decline. It is estimated that by 2020, the operating rate of catalytic cracking units will drop to 68%, and gasoline consumption demand will reach an inflection point. A large number of refining units will be idle, and the transformation to the chemical industry will be the way out for refining companies. [0003] The heavy oil catalytic cracking technology developed by the ...

Claims

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Application Information

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IPC IPC(8): C10G51/00C07C11/06C07C4/06
CPCC10G51/00C07C4/06C10G2400/20C10G2300/70C10G2300/4093C07C11/06Y02P20/52Y02P20/584
Inventor 杨超龚剑洪谢朝钢朱根权沙有鑫成晓洁
Owner CHINA PETROLEUM & CHEM CORP
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